JPH074597B2 - Organic wastewater treatment equipment - Google Patents
Organic wastewater treatment equipmentInfo
- Publication number
- JPH074597B2 JPH074597B2 JP60023078A JP2307885A JPH074597B2 JP H074597 B2 JPH074597 B2 JP H074597B2 JP 60023078 A JP60023078 A JP 60023078A JP 2307885 A JP2307885 A JP 2307885A JP H074597 B2 JPH074597 B2 JP H074597B2
- Authority
- JP
- Japan
- Prior art keywords
- biological treatment
- liquid
- treatment
- membrane
- organic wastewater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Activated Sludge Processes (AREA)
Description
【発明の詳細な説明】 ［産業上の利用分野］ 本発明の有機性廃水の処理装置に係り、特に生物処理手
段と、この生物処理手段からの処理液を膜分離装置する
膜分離装置を備えた有機性廃水の処理装置に関するもの
である。Description: TECHNICAL FIELD The industrial wastewater treatment apparatus of the present invention relates to an organic wastewater treatment apparatus, and particularly includes a biological treatment means and a membrane separation device for separating a treatment liquid from the biological treatment means into a membrane. The present invention relates to an organic wastewater treatment device.
［従来の技術］ 有機性廃水を生物処理し、次いで限定濾過装置等の膜分
離装置によって固液分離するようにした有機性廃水の処
理装置は公知である。[Prior Art] An organic wastewater treatment apparatus is known in which organic wastewater is biologically treated and then solid-liquid separated by a membrane separation device such as a limited filtration device.
第２図は生物処理装置１と膜分離装置２とを備えた従来
の有機性廃水処理装置の構成図である。第２図におい
て、有機性廃水は生物処理装置１に導入され生物処理さ
れた後、配管３を通って膜分離装置２に送られ膜分離処
理され、次いで配管４から処理水として取り出される。
なお、配管３には膜の透過性の維持および汚染軽減のた
めに凝集剤の添加手段10が設けられている。また膜分離
装置２で濃縮された液の一部は返送汚泥として配管５か
ら生物処理装置１へ戻され、濃縮液の残部は配管６から
固液分離装置７に導入され固液分離処理される。固液分
離処理されて生じた汚泥又は脱水ケーキは取付手段８か
ら取り出され、一方分離された液は配管９から取り出さ
れ適宜処理される。FIG. 2 is a configuration diagram of a conventional organic wastewater treatment device including a biological treatment device 1 and a membrane separation device 2. In FIG. 2, the organic wastewater is introduced into the biological treatment apparatus 1 and subjected to biological treatment, then sent through the pipe 3 to the membrane separation apparatus 2 for membrane separation treatment, and then taken out from the pipe 4 as treated water.
The pipe 3 is provided with a coagulant addition means 10 for maintaining the permeability of the membrane and reducing contamination. Further, a part of the liquid concentrated in the membrane separation device 2 is returned as return sludge from the pipe 5 to the biological treatment device 1, and the rest of the concentrated liquid is introduced from the pipe 6 into the solid-liquid separation device 7 for solid-liquid separation treatment. . The sludge or dehydrated cake produced by the solid-liquid separation treatment is taken out from the attachment means 8, while the separated liquid is taken out from the pipe 9 and appropriately treated.
このように生物処理手段と膜分離装置とを併用するよう
にした有機性廃水の処理装置によれば、微生物や酸素が
系外に流出せず、処理効率が高い。また、処理水質が向
上し、かつ安定する等の利点がある。As described above, according to the organic wastewater treatment device in which the biological treatment means and the membrane separation device are used together, the microorganisms and oxygen do not flow out of the system, and the treatment efficiency is high. Further, there are advantages such as improved treated water quality and stability.
［発明が解決しようとする問題点］ しかしながら、膜分離装置で生物処理装置１からの液を
膜分離処理する場合、微生物や酵素以外にも各種の溶解
性の物質（膜が限外濾過膜である場合には分画分子量以
上の溶解性物質）も膜を透過せず、従ってこの溶解性物
質が生物処理系統に戻されるようになる。この溶解性物
質、BOD源にはならないが、CODMn、CODcr、色度等とし
て分析されるものである。また、この溶解性物質は原水
中の生物処理を受けにくい成分或いは生物代謝物などか
ら成り、生物処理系統へ戻されても生物処理を殆ど受け
ず、従って生物処理系統にこの溶解性物質の蓄積が行わ
れる。[Problems to be Solved by the Invention] However, when the liquid from the biological treatment apparatus 1 is subjected to a membrane separation process by the membrane separation device, various soluble substances (the membrane is an ultrafiltration membrane other than microorganisms and enzymes). In some cases, soluble substances above the molecular weight cut-off will also not permeate the membrane, thus allowing the soluble substances to be returned to the biotreatment system. Although it is not a source of soluble substances or BOD, it is analyzed as COD Mn , COD cr , chromaticity, etc. In addition, this soluble substance consists of components or biological metabolites that are difficult to undergo biological treatment in raw water, and hardly undergoes biological treatment even when it is returned to the biological treatment system. Therefore, this soluble substance accumulates in the biological treatment system. Is done.
このような溶解性物質の蓄積は、処理装置の全体構成
が、膜分離装置の濃縮液を生物処理系統に戻さず系外に
排出する一過式のものであれば問題はない。しかし、こ
の一過式の場合、汚泥返送がないため生物処理が不安定
であると共に、高濃縮するので膜の面積を多くとらなく
てはならない。また、生物処理に戻すものにおいての解
決策として、汚泥は濃縮するが、溶解性成分は透過する
膜を利用し、溶解性成分を透過水側に排出する方法、す
なわち膜の分画特性を利用して処理することが提案され
ている。しかし、この場合、膜の選定等が煩雑であると
共に、膜の特性を利用しても膜の目詰まりが激しいた
め、通水時間経過に従い溶解性成分の濃縮が起こり、生
物処理へ戻されて蓄積されてしまう。この目詰り、ある
いは透過性を改善するため凝集剤を膜処理の前に添加す
る方法を採用すれば、このような問題は若干緩和される
ものの通水時間の経過と共に目詰り等がやはり生じ、十
分な対策とはならない。また、凝集剤を系内に添加する
と、保持するMLSS量が増加すると共に、アルカリ度を消
費するので生物処理を好適pHに保つためのNaOH等の使用
量が増加する結果となる。There is no problem with the accumulation of such a soluble substance as long as the entire constitution of the treatment device is of a transient type in which the concentrated liquid of the membrane separation device is discharged to the outside of the system without returning to the biological treatment system. However, in the case of this transient method, biological treatment is unstable because there is no sludge return, and since it is highly concentrated, the area of the membrane must be large. In addition, as a solution for returning to biological treatment, a method is used in which sludge is concentrated but soluble components are permeated, and soluble components are discharged to the permeate side, that is, the fractionation characteristics of the membrane are used. Then, it is proposed to process. However, in this case, the selection of the membrane is complicated, and the membrane is heavily clogged even if the characteristics of the membrane are used, so that the soluble components are concentrated with the passage of water passage time and returned to the biological treatment. It will be accumulated. By adopting a method of adding a coagulant before the membrane treatment in order to improve the clogging or the permeability, such a problem can be alleviated, but the clogging and the like still occur with the passage of water passage time, It is not a sufficient measure. In addition, the addition of a coagulant to the system increases the amount of MLSS retained and consumes alkalinity, resulting in an increase in the amount of NaOH or the like used to keep the biological treatment at a suitable pH.
このように、生物処理手段とこれに接続された膜分離装
置とを備えた有機性廃水の処理装置においては、生物処
理系統における溶解性物質の蓄積、濃縮をできるだけ小
さくする必要がある。As described above, in the organic wastewater treatment apparatus including the biological treatment means and the membrane separator connected to the biological treatment means, it is necessary to minimize the accumulation and concentration of the soluble substance in the biological treatment system.
［問題点を解決するための手段］ 本発明の有機性廃水の処理装置は、有機性廃水を生物処
理し、膜分離装置で処理するよう構成した有機性廃水の
処理装置において、生物処理液の一部を凝集処理し、凝
集汚泥の全量或いは一部を系外に排出するよう構成した
ものであって、 有機性廃水を生物処理する生物処理手段と、該生物処理
手段からの生物処理液が固液分離されることなく導入さ
れる膜分離装置と、該膜分離装置からの濃縮水を生物処
理手段に返送する手段とを備えた有機性廃水の処理装置
であって、前記生物処理手段からの処理液又は膜分離装
置からの濃縮液の一部が分取されて導入されると共に、
無機凝集剤が添加され凝集処理された凝集汚泥の少なく
とも一部を系外に排出する凝集処理装置を設けたことを
特徴とする有機性廃水の処理装置、 を要旨とするものである。[Means for Solving Problems] An organic wastewater treatment apparatus of the present invention is an organic wastewater treatment apparatus configured to biologically treat organic wastewater and treat the treated organic wastewater with a membrane separator. A part of the sludge is coagulated and the whole or part of the coagulated sludge is discharged to the outside of the system. A biological treatment means for biologically treating organic wastewater and a biological treatment liquid from the biological treatment means are provided. A treatment device for organic wastewater, comprising a membrane separation device introduced without solid-liquid separation, and means for returning concentrated water from the membrane separation device to the biological treatment means, the biological treatment means comprising: A part of the treatment liquid or the concentrated liquid from the membrane separation device is collected and introduced, and
An organic wastewater treatment device is characterized in that it is provided with a coagulation treatment device that discharges at least a part of the coagulated sludge that has been subjected to the coagulation treatment by adding an inorganic coagulant.
［作用］ 本発明において、凝集処理装置は、生物処理液あるいは
生物処理液を膜分離したときの濃縮液の一部を凝集処理
し、これに含まれる溶解性成分を凝集固定し、この液中
から分離する作用を働く。そして、凝集処理された汚泥
の全部あるいは一部は、系外に排出される。これによっ
て、生物処理系統における溶解性成分の蓄積、濃縮が抑
制されるのである。[Operation] In the present invention, the coagulation treatment apparatus performs coagulation treatment on a biological treatment liquid or a part of a concentrated liquid obtained by membrane-separating the biological treatment liquid, aggregates and fixes a soluble component contained therein, and Works to separate from. Then, all or part of the coagulated sludge is discharged to the outside of the system. This suppresses the accumulation and concentration of soluble components in the biological treatment system.
［実施例］ 以下図面を参照して実施例について説明する。Embodiments Embodiments will be described below with reference to the drawings.
第１図は本発明の実施例装置の構成図である。この第１
図の装置が第２図の装置と異なるのは、生物処理装置１
からの処理液を膜分離装置２に送る配管３に、分取用の
配管11を接続し、生物処理液の一部を凝集処理装置12に
導入し、凝集された液を配管13から濃縮槽14へ送るよう
構成した点にある。図中15は凝集処理装置12へ凝集剤を
供給するための配管である。その他の構成は第２図の従
来装置と同一であるので、同一部材は同一符号で示され
ている。（なお、本実施例においては、配管３から生物
処理液の一部を取り出すもので説明するが、本発明はこ
れに限定されるものではなく、生物処理装置１、膜分離
装置２、あるいは返送汚泥である濃縮水の配管28から取
り出した液を凝集処理装置12に導入するようにしても良
い。また、生物処理装置１からの処理液としては、生物
混合液でも流出液でも良い。） このように構成された実施例装置において、有機性廃水
は生物処理装置１で生物処理を受け、その処理液の一部
は固液分離されることなく膜分離装置２に導入される。
そして、その処理水（透過液）は配管４から取り出さ
れ、濃縮液は配管５から生物処理装置１に戻される。ま
た、生物処理液の一部（残部）は、凝集処理装置12に導
入され、凝集処理を受けた後、濃縮槽14に導入される。
濃縮槽14で分離された水は配管16から生物処理装置１に
戻され、濃縮槽14で分離された汚泥の一部は返送汚泥と
して配管17、18を経て生物処理装置１に戻される。また
残余の汚泥は余剰汚泥として配管20を経て固液分離装置
７に送られ固液分離処理され、固形分は脱水ケーキとし
て系外に取り出され、分離液は配管19、18を通って生物
処理装置１へ戻される。FIG. 1 is a block diagram of an apparatus according to an embodiment of the present invention. This first
The apparatus shown in the figure is different from the apparatus shown in FIG.
The pipe 11 for separation is connected to the pipe 3 for sending the treatment liquid from the above to the membrane separation device 2, a part of the biological treatment liquid is introduced into the aggregating treatment device 12, and the agglomerated liquid is fed from the pipe 13 to a concentrating tank. It is configured to send to 14. In the figure, reference numeral 15 is a pipe for supplying a coagulant to the coagulation processing device 12. The other components are the same as those of the conventional device shown in FIG. 2, and the same members are designated by the same reference numerals. (In this embodiment, a part of the biological treatment liquid is taken out from the pipe 3, but the present invention is not limited to this, and the biological treatment device 1, the membrane separation device 2, or the returning device is not limited thereto. The liquid extracted from the pipe 28 of concentrated water, which is sludge, may be introduced into the flocculation treatment device 12. Further, the treatment liquid from the biological treatment device 1 may be a biological mixture liquid or an outflow liquid. In the embodiment apparatus configured as described above, the organic wastewater undergoes biological treatment in the biological treatment apparatus 1, and a part of the treated liquid is introduced into the membrane separation apparatus 2 without being subjected to solid-liquid separation.
Then, the treated water (permeate) is taken out from the pipe 4, and the concentrated liquid is returned to the biological treatment apparatus 1 from the pipe 5. Further, a part (remaining portion) of the biological treatment liquid is introduced into the aggregating treatment device 12, subjected to aggregating treatment, and then introduced into the concentrating tank 14.
The water separated in the concentration tank 14 is returned to the biological treatment apparatus 1 from the pipe 16, and a part of the sludge separated in the concentration tank 14 is returned to the biological treatment apparatus 1 as return sludge through the pipes 17 and 18. The residual sludge is sent as excess sludge to the solid-liquid separation device 7 via the pipe 20 for solid-liquid separation treatment, the solid content is taken out of the system as dehydrated cake, and the separated liquid is biologically treated through the pipes 19 and 18. Returned to the device 1.
このように、本実施例装置においては、生物処理液中の
溶解性物質の一部は凝集処理装置12で凝集処理を受け、
汚泥中に取り込まれるようになる。そして、この汚泥は
余剰汚泥として系外に取り出され得るものであるので、
生物処理液からの溶解性物質の分離が可能となり、この
生物処理液中における蓄積が防止されるようになる。As described above, in the apparatus of the present embodiment, a part of the soluble substance in the biological treatment liquid is subjected to the coagulation treatment by the coagulation treatment device 12,
It will be taken into the sludge. And since this sludge can be taken out of the system as excess sludge,
The soluble substance can be separated from the biological treatment liquid, and the accumulation in the biological treatment liquid can be prevented.
本発明において、生物処理装置１としては、好気性処理
方式及び嫌気性処理方式あるいは硝化脱窒処理方法のい
ずれのものも用いることが可能である。In the present invention, as the biological treatment apparatus 1, any of an aerobic treatment method, an anaerobic treatment method, and a nitrification denitrification treatment method can be used.
また、凝集処理装置12にて添加される凝集剤としては、
FeCl3、ポリ硫酸鉄などのFe塩、硫酸バンド、ポリ塩化
アルミニウム（PAC）等のAl塩、その他の無機凝集剤を
用いることができる。またメラミンーホルマリン樹脂等
の有機凝結剤を併用してもよい。Further, as the aggregating agent added in the aggregating treatment device 12,
FeCl 3 , Fe salts such as polyiron sulfate, sulfuric acid bands, Al salts such as polyaluminum chloride (PAC), and other inorganic coagulants can be used. Further, an organic coagulant such as melamine-formalin resin may be used in combination.
なお、生物処理装置１のMLSS濃度の好適に維持するため
に実施例のように凝集汚泥の一部を返送汚泥として配管
19により生物処理装置１に戻しても良い。In addition, in order to maintain the MLSS concentration of the biological treatment apparatus 1 appropriately, a part of the coagulated sludge is piped as return sludge as in the example.
It may be returned to the biological treatment apparatus 1 by 19.
無機凝集剤の添加により固定された溶解性成分の再溶出
は、生物処理の行われるpH範囲では殆どないこと、そし
て、添加された無機凝集剤は生物処理液の一部を取り出
して添加される程度の量であるため生物処理に対して全
く悪影響を及ぼさないことが種々の実験の結果認められ
た。The re-elution of the soluble component fixed by the addition of the inorganic coagulant is hardly in the pH range in which the biological treatment is performed, and the added inorganic coagulant is added after removing a part of the biological treatment liquid. As a result of various experiments, it was found that the amount was moderate and had no adverse effect on biological treatment.
第１図の実施例において固液分離装置７は、余剰汚泥を
処理するためのものであり、余剰汚泥の発生量に見合う
分を濃縮処理している。この固液分離装置７としては、
各種の脱水機を用いることができる。また、この固液分
離装置７によって余剰汚泥の濃縮処理を行う場合には、
高分子凝集剤を汚泥に添加すると一層効果的である。In the embodiment of FIG. 1, the solid-liquid separation device 7 is for treating surplus sludge, and concentrates a portion corresponding to the amount of excess sludge generated. As the solid-liquid separation device 7,
Various dehydrators can be used. Moreover, when performing the concentration process of the excess sludge by this solid-liquid separation device 7,
It is more effective to add a polymer flocculant to the sludge.
なお膜分離装置２としては、限外濾過膜、逆透過膜等の
各種の分離膜を用いた装置を用い得る。限外濾過膜を用
いた装置としては、分画分子量が5000〜200000程度のも
のが好適に用いられるが、この好適な範囲は本発明の範
囲を特に限定するものではない。The membrane separation device 2 may be a device using various separation membranes such as an ultrafiltration membrane and a reverse permeable membrane. As an apparatus using an ultrafiltration membrane, one having a molecular weight cutoff of about 5000 to 200,000 is preferably used, but this preferable range does not particularly limit the scope of the present invention.
また、上記実施例では凝集分離処理した液を配管16、19
で生物処理装置１に戻すようにしているが、配管16を配
管18又は３、あるいは膜分離装置２に接続してもよい。
即ち、本発明では、凝集分離液は、途中経路の如何を問
わず、生物処理手段に戻されればよい。凝集分離液を生
物処理手段に戻す場合、凝集分離液中の溶解性成分の濃
度は著しく少なくなっていると共に、添加された凝集剤
は生物処理または膜分離に対する悪影響を与えない。む
しろ凝集分離液を戻す場合には、膜に対する水量負荷は
増加するが、生物処理液の希釈水とできるので、処理水
質は向上する。なお、凝集分離液を生物処理手段に戻さ
ず、系外に排出して適宜処理しても良い。In addition, in the above-mentioned examples, the liquids subjected to the coagulation separation treatment are pipes 16 and 19
However, the pipe 16 may be connected to the pipe 18 or 3 or to the membrane separation device 2.
That is, in the present invention, the aggregated and separated liquid may be returned to the biological treatment means regardless of the intermediate route. When the coagulated separation liquid is returned to the biological treatment means, the concentration of the soluble component in the coagulated separation liquid is significantly reduced, and the added coagulant does not adversely affect the biological treatment or the membrane separation. On the contrary, when the coagulated separated liquid is returned, the water amount load on the membrane increases, but since it can be used as dilution water of the biological treatment liquid, the treated water quality is improved. The aggregated and separated liquid may be discharged to the outside of the system for proper treatment without returning to the biological treatment means.
以下実験例について説明する。Experimental examples will be described below.
実験例１（従来例） 第２図において、生物処理装置１として活性汚泥処理槽
を用いた。活性汚泥処理槽の容量は1000lであり、MLSS
は10000mg/lである。また、膜分離装置２としてチュー
ブラ型限外濾過膜を用い、濾過膜としては分画分子量20
000のものを用い、入口2.0Kg/cm2、循環水の膜面流速1.
5m/secとした。Experimental Example 1 (Conventional Example) In FIG. 2, an activated sludge treatment tank was used as the biological treatment apparatus 1. The capacity of the activated sludge treatment tank is 1000l, and MLSS
Is 10000 mg / l. A tubular type ultrafiltration membrane is used as the membrane separation device 2, and a molecular weight cutoff of 20 is used as the filtration membrane.
2,000, inlet 2.0Kg / cm 2 , membrane flow velocity of circulating water 1.
It was set to 5 m / sec.
有機性廃水として、BOD10000mg/l、CODMn5500mg/lの除
渣し尿100l/日の割合で活性汚泥処理槽（生物処理槽）
１に投入し曝気した。曝気槽内のCODMn（0.45μｍのメ
ンブレンフィルタ濾過液）は600mg/lであり、余剰汚泥
発生量は600g−DS/日であった。As organic wastewater, activated sludge treatment tank (biological treatment tank) with a ratio of BOD 10000mg / l, COD Mn 5500mg / l depleted urine 100l / day
It was put into 1 and aerated. COD Mn (0.45 μm membrane filter filtrate) in the aeration tank was 600 mg / l, and the amount of excess sludge generated was 600 g-DS / day.
活性汚泥処理槽１からの処理液を膜分離した処理水（透
過液）の初期のCODMnは300mg/lであり、初期の膜分離装
置２の透過流量は1.2m3／m2／日であった。この状態で
運転を継続したところ、１ケ月後の曝気槽内のCOD
Mn（0.45μｍのメンブレンフィルタ濾過液のCODMn）は1
550mg/lとなり、膜分離装置２の処理水のCODMnは600mg/
lとなった。また、濾過流量は0.6m3／m2／日に減少し
た。The initial COD Mn of the treated water (permeate) obtained by membrane separation of the treatment liquid from the activated sludge treatment tank 1 was 300 mg / l, and the initial permeation flow rate of the membrane separation device 2 was 1.2 m 3 / m 2 / day. there were. When operation was continued in this state, COD in the aeration tank after one month
Mn (COD Mn of 0.45 μm membrane filter filtrate) is 1
550mg / l, COD Mn of treated water in the membrane separator 2 is 600mg / l
It became l. The filtration flow rate was reduced to 0.6 m 3 / m 2 / day.
２ケ月後には、曝気槽内のCODMn（0.45μｍのメンブレ
ンフィルタ濾過液）は1900mg/lとなり、膜分離装置２の
処理水のCODMnは720mg/lとなった。また透過流速は0.5m
3／m2／日であった。Two months later, the COD Mn (0.45 μm membrane filter filtrate) in the aeration tank was 1900 mg / l, and the COD Mn of the treated water in the membrane separation device 2 was 720 mg / l. The permeation velocity is 0.5 m
It was 3 / m 2 / day.
３ケ月後も２ケ月後とほぼ同様の運転状態であった。After three months, the operation was almost the same as after two months.
実験例２ 第１図において生物処理装置１と膜分離装置２は実験例
１と同じものを用いると共に、有機性廃水としても上記
実験例１と同じものを用い、この除渣し尿の処理を行っ
た。Experimental Example 2 In FIG. 1, the same biological treatment apparatus 1 and membrane separation apparatus 2 as in Experimental Example 1 were used, and the same organic wastewater as in Experimental Example 1 was used to treat the residual urine. It was
なお、凝集処理装置12に添加する凝集剤としてはFeCl3
を500mg/lasFeの割合で添加した。また配管３から配管1
1へ分取して凝集処理装置12へ導入する曝気槽液は50l/
日とした。その他の条件は上記実験例１と同様にして装
置の運転を行った。The coagulant added to the coagulation treatment device 12 is FeCl 3
Was added at a rate of 500 mg / lasFe. Also pipe 3 to pipe 1
The aeration tank liquid to be collected into 1 and introduced into the coagulation treatment device 12 is 50 l /
It was a day. Other conditions were the same as in Experimental Example 1 above, and the apparatus was operated.
初期のCOD、透過液量等は実験例１と同じであったが、
１ケ月経過後の曝気槽のCODMn（0.45％のメンブレンフ
ィルタ濾過液）は600mg/lであった。また透過液量は1.8
m3／m2／日と逆に増加し、膜分離装置２の処理水のCOD
Mnは270mg/lと初期状態よりも低下していた。なお２ケ
月目及び３ケ月経過後も１ケ月経過後とほぼ同様の結果
であった。Initial COD, permeate volume, etc. were the same as in Experimental Example 1,
COD Mn (0.45% membrane filter filtrate) of the aeration tank after one month was 600 mg / l. The amount of permeated liquid is 1.8
The COD of the treated water of the membrane separator 2 increases in the opposite direction of m 3 / m 2 / day.
Mn was 270 mg / l, which was lower than in the initial state. The results were almost the same after the second and third months, and after the first month.
実験例１及び２の測定結果を比較するために、測定結果
を第３図に示す。The measurement results are shown in FIG. 3 in order to compare the measurement results of Experimental Examples 1 and 2.
第３図より本発明装置によれば長期間に亘って装置を運
転しても生物処理系統におけるCODMnの上昇がなく、透
過液量も十分に確保できることが明らかである。また、
処理水（透過液）の水質も極めて優れたものになること
が明らかである。It is clear from FIG. 3 that the device of the present invention does not increase COD Mn in the biological treatment system even if the device is operated for a long period of time, and a sufficient amount of permeate can be secured. Also,
It is clear that the quality of the treated water (permeate) will be extremely excellent.
［効果］ 以上詳述した通り、本発明の有機性廃水の処理装置によ
れば、生物処理装置からの処理液あるいは膜分離装置か
らの濃縮水の一部が無機凝集剤で凝集処理されて系外へ
排出されるので、生物処理系統における溶存性有機物質
の蓄積等によるCOD成分の上昇が回避され、安定した処
理が可能となる。[Effects] As described in detail above, according to the organic wastewater treatment apparatus of the present invention, a part of the treatment liquid from the biological treatment apparatus or the concentrated water from the membrane separation apparatus is coagulated with an inorganic coagulant to form a system. Since it is discharged to the outside, increase in COD component due to accumulation of dissolved organic substances in the biological treatment system is avoided, and stable treatment becomes possible.
第１図は本発明の実施例装置の構成図、第２図は従来装
置の構成図、第３図は実験例における測定結果を示すグ
ラフである。 １…生物処理装置、２…膜分離装置、７…固液分離装
置、12…凝集処理装置。 14…濃縮槽。FIG. 1 is a block diagram of an apparatus according to an embodiment of the present invention, FIG. 2 is a block diagram of a conventional apparatus, and FIG. 3 is a graph showing measurement results in an experimental example. 1 ... Biological treatment device, 2 ... Membrane separation device, 7 ... Solid-liquid separation device, 12 ... Coagulation treatment device. 14 ... concentration tank.
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ０２Ｆ 9/00 Ｐ 7446−4Ｄ ５０３ Ｃ 7446−4Ｄ (72)発明者 古市 光春 神奈川県横浜市保土ヶ谷区仏向町1723番地 栗田工業株式会社総合研究所内 (72)発明者 一柳 直人 神奈川県横浜市保土ヶ谷区仏向町1723番地 栗田工業株式会社総合研究所内 (56)参考文献 特開 昭55−155798（ＪＰ，Ａ) 特開 昭56−84697（ＪＰ，Ａ) 特開 昭52−146050（ＪＰ，Ａ)─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification number Reference number within the agency FI Technical display location C02F 9/00 P 7446-4D 503 C 7446-4D (72) Inventor Mitsuharu Furuichi Hodogaya, Yokohama, Kanagawa Prefecture 1723, Kuroda Industry Co., Ltd., Research Center, Bukko, Choku-ku (72) Inventor Naoto Ichiyanagi 1723, Hokkokai-cho, Hodogaya-ku, Yokohama-shi, Kanagawa Kurita Kogyo Co., Ltd. (56) Reference JP-A-55-155798 A) JP-A-56-84697 (JP, A) JP-A-52-146050 (JP, A)
Claims (1)
と、該生物処理手段からの生物処理液が固液分離される
ことなく導入される膜分離装置と、該膜分離装置からの
濃縮水を生物処理手段に返送する手段とを備えた有機性
廃水の処理装置であって、前記生物処理手段からの処理
液又は膜分離装置からの濃縮液の一部が分取されて導入
されると共に、無機凝集剤が添加され凝集処理された凝
集汚泥の少なくとも一部を系外に排出する凝集処理装置
を設けたことを特徴とする有機性廃水の処理装置。1. A biological treatment means for biologically treating an organic wastewater, a membrane separation device into which a biological treatment liquid from the biological treatment means is introduced without solid-liquid separation, and concentrated water from the membrane separation device. And a means for returning to the biological treatment means, wherein a part of the treatment liquid from the biological treatment means or the concentrated liquid from the membrane separation device is collected and introduced. An apparatus for treating organic wastewater, comprising a coagulation treatment device for discharging at least a part of coagulation sludge to which an inorganic coagulant has been added and subjected to coagulation treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60023078A JPH074597B2 (en) | 1985-02-08 | 1985-02-08 | Organic wastewater treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60023078A JPH074597B2 (en) | 1985-02-08 | 1985-02-08 | Organic wastewater treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61181595A JPS61181595A (en) | 1986-08-14 |
| JPH074597B2 true JPH074597B2 (en) | 1995-01-25 |
Family
ID=12100377
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60023078A Expired - Fee Related JPH074597B2 (en) | 1985-02-08 | 1985-02-08 | Organic wastewater treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH074597B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10148474A1 (en) * | 2001-10-01 | 2003-05-08 | Koehler August Papierfab | Process and device for cleaning waste water |
| JP5120008B2 (en) * | 2008-03-25 | 2013-01-16 | 栗田工業株式会社 | Biological treatment method of water containing organic matter |
| JP5728662B2 (en) * | 2009-03-27 | 2015-06-03 | 日之出産業株式会社 | Wastewater treatment of hydrophilic polymer colloid materials |
| WO2018194690A1 (en) * | 2017-04-21 | 2018-10-25 | General Electric Company | Systems and methods for upgrading conventional activated sludge plants |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52146050A (en) * | 1976-05-29 | 1977-12-05 | Sanki Eng Co Ltd | Process for waste water with high concentration of organic component |
| JPS55155798A (en) * | 1979-05-23 | 1980-12-04 | Ebara Infilco Co Ltd | Treating method of organic waste water |
| JPS5684697A (en) * | 1979-12-08 | 1981-07-10 | Ebara Infilco Co Ltd | Treatment of high concentration organic waste water |
-
1985
- 1985-02-08 JP JP60023078A patent/JPH074597B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61181595A (en) | 1986-08-14 |
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